过滤除尘设备论文

① 除尘器论文怎么写啊~~

网上搜啊 很多的

② 除尘设备的除尘机理是什么，可以分为几种类型

除尘器的唯一功能是将粉尘从含尘气流中分离出来。根 据粉尘特性及尘粒在气体中的运动规律设计并制造各种除尘器， 其除尘机理是利用重力、离心运动、惯性碰擦、静电力、筛分、 扩散、镶嵌等作用。
(1) 重力。地球上所有物体均处于地心引力之下。含尘气体 中的尘粒在重力作用下自然沉降，粉尘即从含尘气体中分离出来。 (2) 离心运动。做旋转运动的含尘气体，在合外力突然消失 或者不足以提供圆周运动所需向心力的情况下，做逐渐远离圆心 的运动，即离心运动。
如果做旋转运动的含尘气流其各个部分间 的作用力不足以提供使尘粒做圆周运动所需的向心力，则含尘气 流中的粉尘将做离心运动，于是粉尘从旋转中的气流中被甩出来， 即尘气分离。 (3) 惯性碰撞。
任何物体均有保持固有惯性的特点。尘粒也 是物体，当其运动中受大阻力时，含尘气流将改变方向，微小尘 粒因质量小，可随气流一起运动。而质量大者，由于惯性大，所 以保持原来运动方向。这样，尘粒较大者即从含尘气流中分离 出来。
(4) 筛分。当含尘气流通过过滤时，粉尘粒径大于滤料孔隙 尺寸，则尘粒被滤料阻留下来，而小于滤料孔隙尺寸的尘粒通过 滤料，这就是筛分。 (5) 镶嵌与架桥。由于粉尘形状各异，尺寸大小不一，所以 滤料孔隙尺寸也各不相同。
当粉尘某个方向的尺寸正好与滤料孔隙某一部分尺寸相当时，则因尘粒与滤料孔隙的摩擦阻力而被卡 在孔隙尺寸相当的部位上，这就是镶嵌；也可能有限细长针状尘 粒横搭在孔隙的狭窄部位中，这就是架桥，从而使滤料孔隙变得 越来越小。
(6) 扩散。在含尘气流中，有些很微细的尘粒，像气体分子 一样做布朗运动，这就增加了与集尘物体表面接触或碰撞的机会， 使尘粒被捕获。(7) 静电力。
悬浮于空气中的微细固体颗粒由于某些原因总 有可能带上电荷，当带有电荷的粉尘通过电场时，会因为异性电 相吸引而被捕获。

③ 跪求布袋除尘系统的设计！文章也好，连接也可以！谢！

先，我们要知道布袋除尘器的过滤原理，因为下面所讲得就是过滤的问题！过滤原理：含尘气体由进风口进入，经过灰斗时，气体中部分大颗粒粉尘受惯性力和重力作用被分离出来，直接落入灰斗底部。

布袋除尘器作为一种高效除尘设备，目前已广泛应于各工业部门。近年来，随着国民经济的发展以及愈来愈严格的环境保护要求，布袋除尘器在产量上有了相当大的增长，品种也日渐增多。因此，在设计工作中合理地选定布袋除尘器的基本参数，正确地进行除尘系统设计，不仅对于控制污染、保护环境有重要作用，而且对于提高设备处理含尘气体的能力，降低设备投资从而减少工程造价，也具有极重要的经济意义。

选择布袋除尘器时，我们要过滤风速问题，这是一项较复杂的工作，它与粉尘性质、含尘气体的初始浓度、滤料种类、清灰方式有密切的关系。

从设计角度讲，应该也可以抓住主要问题进行分析。这是因为，目前国内产品中可供选择的滤料种类及其清灰方式相对讲不是很多，滤料及其清灰方式相应地易于确定；至于初始尘浓，除了工艺提供资料外，或经实测取得一手数据，或按设计者的经验确定。这就是说，影响过滤风速的尘浓、滤料及清灰方式三个因素相对的说较易合理地确定。正确选择过滤风速的关键，首先在于弄清粉尘及含尘气体的性质，其次要正确理解和认识过滤风速与除尘效率、过滤阻力、清灰性能三者之间的关系。经过分析，现在知道怎么设计布袋除尘器了吧！

④ 需求一篇关于高炉煤气除尘的文章或论文

锅炉控制系统设计 锅炉控制系统设计

40页 1.8万字

为了减少大气污染和节约能源，燃气锅炉正在逐步取代燃煤锅炉供电、供热，如热电厂既供热又发电等等，特别在大型冶金企业生产过程中产生的各种煤气，如高炉煤气、焦炉煤气、转炉煤气等现在基本上都已回收利用。由于各个企业经济、技术等条件的不同，能源的利用程度等也是有差别的。由于控制不当，有的甚至产生严重的大气污染。
本设计是对一家石化厂燃煤蒸汽锅炉控制系统的改造。将变频调速技术与智能控制技术相结合，设计成以烧瓦斯为主、烧煤为辅的控制系统。针对燃烧过程的特性，借助变频器能无级调速和节能，并且有很好的动态跟踪的特性，可以实现输入的空气量自动跟踪燃气量和燃质的变化。再加上智能控制策略可以解决瓦斯气燃烧过程中的数学建模问题，就很好地实现了燃烧过程的优化。本设计还可以实现远程控制，保证了工作过程中的高效、及时和安全性。

1 绪 论 1
1.1 锅炉控制研究的背景和意义 1
1.2 国内外蒸汽锅炉控制的研究状况及其发展 1
1.2.1 蒸汽锅炉控制系统的发展 2
2 总体方案 5
2.1 原蒸汽锅炉的状况 5
2.2 主控制对象和设备 5
2.2.1 锅炉系统 5
2.2.2 控制方案 5
2.3 下位机 6
2.3.1 功能 6
2.3.2 控制流程图 7
2.4 工艺流程 7
3 模糊控制的产生和应用 9
3.1 模糊控制的产生和发展 9
3.2 基本模糊控制器的设计 10
4 硬件配置 14
4.1 触摸屏 14
4.1.1 触摸屏的工作原理 14
4.1.2 Pro-face触摸屏 14
4.2 S7-200 PLC 15
4.2.1 机械结构特性 15
4.2.2 CPU226 15
4.2.3 EM235模块的特点 17
4.3 变频器 18
4.3.1 变频器的基本结构 18
4.3.2 EV 1000 18
4.3.3 EV 2000 18
4.4 其它相关硬件 19
4.4.1 接触器 19
4.4.2 中间继电器 19
4.4.3 火焰检测器 19
4.4.4 按钮 19
4.4.5 开关电源 20
5 硬件控制设计 21
5.1 出渣电机控制 22
5.2 引风风机控制 22
5.3 鼓风风机控制 23
5.4 送煤电机控制 23
5.5 其它相关硬件的控制 23
5.5.1 瓦斯阀 23
5.5.2 炉排控制 24
5.6 硬件间的通信 24
6 软件设计 26
6.1 触摸屏界面 26
6.2 PLC资源配置 26
6.2.1 PLC的输入/输出示意图 26
6.2.2 开关量输入/输出地址 27
6.3 PLC程序控制 28
6.3.1 程序控制流程略图 28
6.3.2 PLC程序 29
结 论 35
致 谢 36
参考文献 37

部分参考文献：

张万忠 可编程控制器应用技术 北京 化学工业出版社
于庆广 可编程控制器原理及系统设计 北京 清华大学出版社
林小峰 可编程控制器原理及应用 北京 高等教育出版社
钟肇新 可编程控制器原理及应用 广州 华南理工大学出版社

全文下载可以看我的微博 http://t.qq.com/baobee 也可以QQ问我～

⑤ 急求有关除尘器的英语论文

Experimental study of electrostatic precipitator
performance and comparison with existing
theoretical prediction models
S.H. Kim, K.W. Lee*
Kwangju Institute of Science and Technology, Department of Environmental Science and Engineering,
1 Oryong-dong, Puk-gu, Kwangju 500-712, South Korea
Received 1 February 1999; received in revised form 21 May 1999; accepted 2 June 1999
Abstract
A laboratory-scale single-stage electrostatic precipitator (ESP) was designed, built and
operated in a wind tunnel. As a "rst step, a series of experiments were concted to seek the
operating conditions for increasing the particle collection e$ciency by varying basic operating
parameters including the wire-to-plate spacing, the wire radius, the air velocity, the turbulence
intensity and the applied voltage. As the diameter of the discharging wires and the wire-toplate
spacing are set smaller, the higher collection e$ciency has been obtained. In the
single-stage multiwire ESP, there exists an optimum wire-to-wire spacing which provides
maximum particle collection e$ciency. As the air velocity increases, the particle collection
e$ciency decreases. The turbulent #ow is found to play an important role in the relatively low
electric "eld region. In the high electric "eld region, however, particles can be deposited on the
collection plates readily regardless of the turbulence intensity. The experimental results were
compared with existing theories and Zhibin and Guoquan (Aerosol Sci. Technol. 20 (1994)
169}176) was identi"ed to be the best model for predicting the ESP performance. As the second
step, the in#uence of particle contamination at the discharging electrode and at the collection
plates were experimentally measured. The methods were sought for keeping the high collection
e$ciency of ESP over elapsed time by varying the magnitude of rapping acceleration, the time
interval between raps, the types of rapping system (hammer/vibrator) and the particle reentrainment.
The rapping e$ciency and the particle re-entrainment were increased with
increasing magnitude of rapping acceleration and time interval between raps. However, when
the thickness of deposited #y ash layer is su$ciently high, the concentration of re-entrained
particles starts decreasing abruptly e to the agglomeration force which can interact among
0304-3886/99/$ - see front matter ( 1999 Elsevier Science B.V. All rights reserved.
PII: S 0 3 0 4 - 3 8 8 6 ( 9 9 ) 0 0 0 4 4 - 3
deposited particles. The combined rapping system is found more e!ective for removing
deposited particles than the hammer rapping system only. ( 1999 Elsevier Science B.V. All
rights reserved.
Keywords: Electrostatic precipitation; Turbulent #ow; Rapping; Particle re-entrainment; Collection e$-
ciency; Negative corona
1. Introction
Electrostatic precipitators (ESPs) are one of the most commonly employed
particulate control devices for collecting #y ash emissions from boilers, incinerators
and from many other instrial processes. They can operate in a wide range of
gas temperatures achieving high particle collection e$ciency compared with mechanical
devices such as cyclones and bag "lters. The electrostatic precipitation process
involves several complicated and interrelated physical mechanisms: creation
of a non-uniform electric "eld and ionic current in a corona discharge, ionic
and electronic charging of particles moving in combined electro- and hydrodynamic
"elds, and turbulent transport of charged particles to a collection
surface.
Generally, the collection e$ciency of ESP decreases as the discharging electrode
and collection plates are contaminated with particulates. Thus, a rapping system is
needed for removing the collected particulates periodically. While there have been
numerous theoretical and experimental studies on particle collection characteristics of
electrostatic precipitators, a relatively small number of the studies addressed the
e!ects of particle accumulation both at the discharging electrodes and at the collection
plates. Both phenomena are known to in#uence adversely the performance of
electrostatic precipitators. Many researchers, such as Deutsch [1], Cooperman [2],
Leonard et al. [3], Khim et al. [4], Zhibin and Guoquan [5], and Kallio and Stock
[6], concted particle collection measurements of ESP. However, they concentrated
mostly on the e!ects of both turbulent mixing and secondary wind in multiwire
single-stage electrostatic precipitators. Speci"cally, Cooperman [2] considered reentrainment
and longitudinal turbulent mixing e!ects, Leonard et al. [3] the "nite
di!usivity, and Zhibin and Guoquan [7] the non-uniform air velocity pro"le. Among
them, only Zhibin and Guoquan [7] measured the collection e$ciency of a singlestage
ESP covering a wide particle size range. Even though their experimental data
are considered to be practical and useful, their experimental conditions were not
identi"ed clearly.
In the present study, well-de"ned collection e$ciency data for an ESP are presented
covering the particle size range of 0.1}100 lm. The particles used in the present study
came from the Bo-Ryung power plant in Korea. In addition, the ESP performance
was evaluated in terms of optimum operating conditions. Finally, the optimum
rapping conditions were sought under which the rapping e$ciency increases and the
particle re-entrainment decreases.
4 S.H. Kim, K.W. Lee / Journal of Electrostatics 48 (1999) 3}25
Fig. 1. Schematic diagram of the wind tunnel for the eight wired single-stage ESP performance test.
2. Review of theoretical models
2.1. Particle charging
Fig. 1 shows the laboratory-scale electrostatic precipitator. The particle charging
system consists of discharge wires with diameter (D8) and two grounded parallel
plates of length (¸). A high negative voltage (<8) is applied to the corona discharge
wires, and suspended particles of diameter (d1) #ow with air between the plates at
a velocity (;) in the y-direction. In the whole range of particle sizes, both "eld
charging and di!usion charging mechanisms contribute to signi"cant charges [8,9].
In these theoretical analyses, it is nearly correct to sum the rates of charging from the
two mechanisms and then solve for the particle charging as follows:
dq1
dt
"q4
q A1!q
q4B2#d21
eN
0
4 S8k¹p
m
expA! 2qe
d1k¹B (1)
where q1 is the particle charge, q4 is the saturation charge,N
0 is the average number of
molecules per unit volume, e is the electronic charge ("1.6]10~19 C), b is the ion
mobility ("1.4]10~4 m2/V s), e0 is the permittivity of free space ("8.85]
10~12 F/m), d1 is the diameter of particle, k is the Boltzmann constant ("1.38]
10~23 J/K), ¹ is the absolute temperature ("293 K), m is the mass of a particle
("(p/6)d31
o1), and o1 is the particle density ("2.25]103 kg/m3).
2.2. Theoretical models of particle collection ezciency
Theoretical models of ESPs were provided by Deutsch [1], Cooperman [2],
Leonard et al. [3], Zhibin and Guoquan [7] and others. The Deutsch model for
S.H. Kim, K.W. Lee / Journal of Electrostatics 48 (1999) 3}25 5
calculating the particle collection in an ESP assumes complete mixing by turbulent
#ow and thereby uniform concentration pro"les. In order to improve the drastic
assumption of in"nite di!usivity in the Deutsch model, many researchers tried to
develop "nite di!usivity models by dealing with the convective-di!usion equation
with various boundary conditions.
Cooperman [2] developed a theory which modi"es the Deutsch model to account
for the e!ects of turbulence and particle turbulent di!usion. The major limitations of
the Cooperman model lie absence of a general method to estimate the re-entrainment
factor and the particle di!usivity. Leonard et al. [3] developed a more complicated
two-dimensional model using the method of the separation of variables from the
convective-di!usion equation. He assumed uniformity of velocity components of
charged particles and particle di!usivity. This assumption fails to adequately describe
the particle di!usivity near the collection plates, where it is governed mainly by the
molecular transport and, therefore, the di!usivity near the wall is signi"cantly lower
than the di!usivity in the turbulent core. Zhibin and Guoquan [7] suggested a new
model for the single-stage ESP which takes into account the e!ect of turbulence
mixing by electric wind. Predicted collection e$ciencies of the above theoretical
models are summarized as follows:
gDe"1!exp(!De), (2)
gCoo"1!expC;¸
2D
!SG A;¸
2DB2#(1!R)PeA¸
=B2HD, (3)
gLeo"1!P1
0
PA m!De
J2De/PeBdm, (4)
gZhi"1!S Pe
4pDeP1
0
expC!Pe
4De
(m!De)2Ddm, (5)
where <t is the migration velocity ("q1EC#/3pkd1), C# is the slip correction factor
("1#(2/Pd1)[6.32#2.01 exp(!0.1095Pd1)]), P is the absolute pressure
("76 cm Hg), E is the electric "eld intensity ("<8/=),= is the width of wire-toplate,
De is the Deutsch number ("<t¸/;=), Pe is the electric Peclet number
("<t=/D1), D1 is the particle di!usivity, and P(z) in Eq. (4) is the Gaussian probability
distribution function given by
P(z)" 1
J2pPz
~=
expA!B2
2 BdB. (6)
In order to evaluate the particle di!usivity for the calculation of De and Pe, the #ow
is assumed to be a fully developed turbulent channel #ow. The related physical
quantities are speci"ed like below [10]
1
f 1@2
"!1.8 log10A6.9
ReB, ;q
"Sf;2
8
,
D5"0.12;q=, DB"k¹C#
3pkd1
, D1"D5#DB (7)
6 S.H. Kim, K.W. Lee / Journal of Electrostatics 48 (1999) 3}25
Fig. 2. Comparison of measured fractional number of particles with existing theoretical predictions.
Experimental conditions: D8"1 mm, <8"50 kV, Sx"150 mm, Sy"37.5 mm, ;"1 m/s, ¹6"12%.
where f is the friction factor, Re is the Reynolds number ("2;=/v), ;q is the friction
velocity, D5 is the turbulent di!usivity, and D
B is the Brownian di!usivity.
With the measured data of fractional number of particles at the inlet of the
single-stage ESP, measured fractional number of particles at the outlet of the singlestage
ESP was compared with calculated results of each theoretical prediction model
as shown in Fig. 2. The grade e$ciency is computed over the particle size range
0.1}100 lm, and then integrated the grade e$ciency to obtain the overall mass
e$ciency, where the particle size distribution function is assumed to be lognormal.
The size distribution of most polydisperse aerosols is found very close to the lognormal
distribution. Thus, this assumption is quite reasonable. The lognormal particle
size distribution function is given by Herdan [11]:
f (d)" 1
d ln p'(2p)0.5
expC!(ln d!ln d')2
2 ln2 p' D (8)
where :=
0
f (d)dd"1, the geometric mean diameter d'"5.03 lm and the geometric
standard deviation p'"1.73 from the measured data. The fraction number of each
particle size at the outlet of ESP can be described by this particle size distribution
function. Finally, the theoretical overall collection e$ciency is calculated for comparison
with the experimental results.
S.H. Kim, K.W. Lee / Journal of Electrostatics 48 (1999) 3}25 7
Table 1
The dimensions and operating conditions for the present eight wire single-stage ESP
Dimensions and operating conditions Values
Diameter of discharge wire, D8 (mm) 1, 2, 3, 4
Wire-to-plate spacing, Sx (mm) 50}200
Wire-to-wire spacing, Sy (mm) 12.5}50
Length of collection plate, ¸ (m) 0.75
Height of collection plate, H (m) 0.3
Air #ow velocity, ; (m/s) 0.8}2.5
Applied voltage on wires, <8 (kV) 10}70
Turbulence intensity, ¹6 (%) 12, 15, 18
Air temperature, ¹ (K) 293
Air pressure, P (atm) 1
3. Experimental procere
The experimental apparatus used in this study consisted of six components: an
aerosol generation system, a wind tunnel, a laboratory-scale ESP, a rapping system,
an aerosol sampling system, and a particle concentration measurement system. The
ESP was 30 mm (=)]500 mm (H)]750 mm (¸) in size and was equipped with eight
discharge wires. The schematic diagram of the ESP is shown in Fig. 1. The basic
operating conditions of the ESP and the parameters used are shown in Table 1. The
single-lane wind tunnel was made of plexiglas and operated at the ambient temperature.
It can provide air velocities ranging from 0.1 to 6 m/s. A thermo-anemometer
(Model 8525, Alnor Instrument Company) was used to measure the air velocity. The
air "ltered with a high e$ciency particulate "lter (HEPA) was supplied with a turbulence
intensity of about 12% and at a "xed mean velocity of 1 m/s. The #y ash
particles which came from the Bo-Ryung electric power plant in Korea were dispersed
using a microst feeder (Model MF-2, Sibata Scienti"c Technology Ltd.). The #y ash
was analyzed using chemical, physical and electrical methods and the analysis results
are shown in Table 2. The microst feeder utilizes a variable-speed turntable to
transport #y ash at a constant rate to the test section in the wind tunnel. The
laboratory-scale single-stage ESP described previously was installed in the test section
as shown in Fig. 1. For aerosol sampling, an isokinetic sampling tube was used to
measure the concentration and the size distribution of the #y ash particles. The
measuring points were positioned at the center of the cross-sectional area of the wind
tunnel. Measurements of the particle concentrations upstream and downstream were
made by Aerosizer (Model Mach II and LD, API) which is capable of measuring
indivially the size of particles in the range of 0.2}200 lm regardless of the particle
shapes. Finally, the overall collection e$ciency, g%91, was evaluated with the mass
loading of the particles measured at inlet and outlet of the ESP:
g%91"[(m)*/-%5!(m)065-%5]
(m)*/-%5
, (9)
8 S.H. Kim, K.W. Lee / Journal of Electrostatics 48 (1999) 3}25
Table 2
Results of chemical, physical, and electrical analysis of #y ash
Classi"cation Values
Chemcial components of #y ash SiO2 (46.47 wt%)
Al
2
O
3
(24.48 wt%)
Fe2O3 (15.28 wt%)
CaO (4.06 wt%)
MgO (1.56 wt%)
Na2O (0.35 wt%)
K2O (1.17 wt%)
SO
3
(4.20 wt%)
TiO2 (1.18 wt%)
Measurement of particle size distribution GMD 5.03 m
GSD 1.73
d1)4.23 lm
d1'4.23 lm
Electrical resistivity 4.3]109 () m)
where (m)*/-%5 is the mass loading of particles at the ESP inlet. (m)065-%5 is the mass
loading of particles at the ESP outlet.
Presently, two philosophies are prevalent with regard to removal and transfer of the
particulate from the collection plates.

⑥ 水过滤除尘器原理除尘的效率

含尘气体从设备顶部进风口进入设备后，以高速经过旋风分离器，使含尘气体沿轴线调整螺旋向下旋转，利用离心力，除掉较粗颗粒的粉尘，有效地控制了进入电场的初始含尘浓度。然后，气体经下灰斗进入电场工作，由于下灰斗截面积大于内管截积数倍，根据旋转矩不变原理，径向风速和轴向风速急剧降低产生零速界面而使内管中的重颗粒粉尘沉降于下灰斗内，降低了进入电场的粉尘浓度，低浓度含尘气体经电收尘而凝聚在阴阳极板上，经清灰振打而将收集的粉尘由锁风排灰装置输送走。为了防止内管旋风和电场极板振打后在下灰斗内形成的二次扬尘，特在下灰斗中设置了隔离锥。

⑦ 过滤式除尘器有什么特点

过滤式除尘器，是一种干式高效除尘器，它是利用纤维编制物制作的袋式过滤元件来捕集含尘气体中固体颗粒物的除尘装置。其作用原理是尘粒在绕过滤布纤维时因惯性力作用与纤维碰撞而被拦截。细微的尘粒（粒径为１微米或更小）则受气体分子冲击（布朗运动）不断改变着运动方向，由于纤维间的空隙小于气体分子布朗运动的自由路径，尘粒便与纤维碰撞接触而被分离出来。其工作过程与滤料的编织方法、纤维的密度及粉尘的扩散、惯性、遮挡、重力和静电作用等因素及其清灰方法有关。滤布材料是布袋除尘器的关键，性能良好的滤布，除特定的致密度和透气性外，还应有良好的耐腐蚀性、耐热性及较高的机械强度。耐热性能良好的纤维，其耐热度目前已可达到连续温度１９０℃，瞬间温度２００℃。

⑧ 求一份完整的袋式除尘系统设计的论文

先去知网下载，研究下别人怎么写的，从中提炼出来自己的东西就可以了，不会找的话，可以去我qq空间里看下论文的查找步骤

⑨ 除尘设备有哪些分类及原理

除尘设备按照工作原理分为5类
一、机械式除尘设备
机械式除尘设备包括重力除尘设备、离心除尘设备和惯性除尘设备，下面以重力除尘设备为例简介
重力除尘设备又分为碰撞式和回转式，前者沿是气流方向设一道或多道挡板，含尘气体碰撞到挡板上使尘粒从气体中分离出来。显然，气体在撞到挡板之前速度越高，碰撞后越低，则携带的粉尘越少，除尘效率越高。后者是使含尘气体多次改变方向，在转向过程中把粉尘分离出来。气体转向的曲率半径越小。转向速度越高，则除尘效率越高。
在实际应用中，惯性除尘设备一般放在多级除尘系统的第一级，用来分离颗粒较粗的粉尘。它特别适用于捕集粒径大于10μm的干燥粉尘．而不适宜于清除粘结性粉尘和纤维性粉尘。
二、洗涤式除尘设备
洗涤式除尘设备包括水浴式除尘设备、泡沫式除尘设备，文丘里管除尘设备、水
膜式除尘设备等，下面以水浴式为例简介：
水浴式除尘设备工作原理是在除尘设备内水通过喷嘴喷成雾状，当含尘烟气通过雾状空间时，因尘粒与液滴之间的碰撞、拦截和凝聚作用，尘粒随液滴降落下来。
水浴式除尘设备优点：内设很小的缝隙和孔口，可以处理含尘浓度较高的烟气而不会导致堵塞，而且过滤水可以循环使用，直至洗涤液中物质浓度达到相当高的浓度为止，简化了水处理设施；缺点：设备体积较大，处理细粉尘的能力较低。所以该类型除尘器常用于处理粉尘径大含烟浓度较高的烟气
三、过滤式除尘设备
过滤式除尘设备除尘机理类似于口罩，是通过过滤材料对空气中的飞灰颗粒进行机械拦
截来实现的，另先收到的飞灰颗粒在滤料表面形成了一层粘稠的稳定的灰层，称为滤饼或虑床，它又起了很好的过滤作用。过滤元件可以由棉毛纤维、玻璃纤维或各种化学纤维经过纺织（或针刺）成滤料，再缝制成垂直悬挂的滤袋，不同场合要选用不同的滤料。在滤袋上收集到的粉尘通过周期性的机械抖动、过滤后的烟气反吹或压缩空气的脉冲反吹等途径使布袋变形而将灰清除。
四、静电除尘设备
静电除尘设备的工作原理是烟气通过电除尘设备主体结构前的烟道时，使其烟尘带正电荷，然后烟气进入设置多层阴极板的电除尘设备通道。由于带正电荷烟尘与阴极电板的相互吸附作用，使烟气中的颗粒烟尘吸附在阴极上，定时打击阴极板，使具有一定厚度的烟尘在自重和振动的双重作用下跌落在电除尘设备结构下方的灰斗中，从而达到清除烟气中的烟尘的目的。
电除尘设备主要应用于火力发电厂，作用是将燃灶或燃气锅炉排放烟气中的颗粒烟尘目的。
五、磁力除尘设备
磁力除尘设备原理是利用导电线圈产生磁场，吸附磁性颗粒，主要用于钢铁等工业废气，这些废气中的尘粒约有70％以上具有强磁性，因此可以使用磁力过滤器，将带磁性颗粒从气体中吸出，净化空气。

⑩ 布袋除尘器的过滤作用由哪些效应产生

布袋除尘器是利用多孔纤维材料的过滤作用将含尘气体中的粉尘过滤出来的。这种过滤作用通常由下列效应而产生。
1、筛滤效应：当粉尘的粒径大于滤袋纤维间隙或滤袋上已粘附的粉尘层的孔隙时，尘粒无法通过滤袋，就被截留下来。这种效应称为筛滤效应。通常的滤料，这种筛滤效应是很小的，因为滤袋纤维间的空隙往往要比尘粒大得多。只有当滤袋上积沉一定数量的粉尘并形成粉尘层后，筛滤效应才显示出来。
2、碰撞效应：当含尘气体靠近滤袋纤维时，空气绕纤维而过，但较大的尘粒由于其惯性价用而偏离气流方向，撞击到纤维上而被截留的效应称为碰撞效应。
3、钩住效应；当含尘气体接近滤袋纤维时，如果靠近纤维的尘粒部分突入纤维边缘时，尘粒就有可能被纤维边缘钩住，这种效应叫做钩住效应。
4、扩散效应；当尘粒的直径为0.2微米以下时，由于气流的气体分子的相互碰撞而偏离气流流线作不规则的布朗运动，这就增加了尘粒与纤维的碰撞机会，使尘粒彼捕获。由于布朗运动引起的扩散，使粉尘微粒与滤料接触吸附的作用，叫做扩散效应。尘粒越小，这种不规则的运动越剧烈，则尘粒与纤维的碰撞接触的机会也越多。
5、静电效应：当尘粒与滤料纤维的电荷相反时，尘粒就会吸附于滤袋上，如果尘粒与滤料的荷电相同，滤袋就排斥尘粒，降低收尘效率。